Process and apparatus for fractionating



Nov. 21, 1939. M. R. FENSKE 2,180,512

PROCESS AND APPARATUS FOR FRACTIONATING Nov. 21, 1939. v M. R. FENsKE PROCESS AND APPARATUS FOR FRACTIONATING Filed Aug. 7, 1937 2 sheets-'sheet 2 Patented Nev. 21, 1939 2,180,512 PROCESS AND APPARATUS FOR FRACTION- ATING Merrell n. Fenske, state couege, to The Pennsylvania Research State College, Pa., vania Pa., assigner Corporation,

a corporation of Pennsyl- Aplilication August 7,1937, Serial No. 157,926 9 Claims. (Cl. 196-94) This invention pertains to a method and ratus for fractional distillation.

In copending application, Serial No. 157,925, led August 7, 1937, by Merrell R. Fenske, there is described and claimed a method and apparatus for fractional distillation wherein high eiciencies are obtained by eiectually contacting ascending vapors with descending reux without serious channeling. This is accomplished generally speaking by conducting the reux down through the zone of contact with ascending vapors in lm form and in separate streams over a plurality of attenuated packing members.

In one species in said copending application the appapacking members are separately enclosed, for in- I stance, by tubes having relatively small cross sections of any desired geometrical shape so that the ascending vapors are brought into eicient contact with the descending reflux in a plurality of separate countercurrently flowing streams or in other words in. a plurality of separate fractionating units.

In said copending application the ascending vapors and/or descending reflux may be'metered into each unit in a manner so that the rectied vapors produced by any one unit will be of substantially the same composition as the rectified vapors produced by any other unit.

This invention comprises an improvement over said copending application in that the amount of descending reflux in each fractionating unit is dependent upon the operation of the least efIicient fractionating unit. In other words the least eicient fractionating unit operates with a reflux ratio suiiiciently high so that the composite product has the desired vtemperature spread. Consequently the reflux ratios obtaining in the remaining tubes will vary so that the composite rectified vapors will be within the desired temperature spread.

Further features -of the invention reside in the construction, arrangement and combination of parts, and in the steps, combinations of steps and sequences' of steps, all of which, together with other features, will become more apparent. to persons skilled in the art as the specification proceeds and upon reference to the drawings in which:

Figures 1a and 1b comprise a sectional elevation (shown broken) illustrating the invention;

Figure 2 is a section on line 2 2 of Figure 1a;

Figure 3 is a section on line 3 3 of Figure 1b;

Figure 4 is a section'on line 4 4 of Figure 1b; and

Figure 5 is a section on line 5 5 of Figure 1b.

For convenience in description, tower I will be referred to as being made up of sections AA, BB, and CC.

Section BB, a part of which is shown in Figure 1a and another part in Figure 1b, comprises i ited '20. Immediately above plate 23 a plurality of tubular members II having their ends mounted in tube sheets I2 and I3. Tube sheets l2 and I3 are illustrated for convenience as being integral with tively. Tubes II may have a cross section of any desired geometrical configuration and up to certain limits of any desired cross sectional area. The cross section of tubes II is preferably limto an area suiiiciently small to prevent serious channeling after the contacting means, for instance packing I6, has been arranged therein.

The preferablelimiting cross sectional area for tubes I I will be not only a .function of the type of 'packing employed since certain forms will as a rule permit the use of a larger cross section without an inordinate falling oif of` efficiency than other forms but also of the degree of -uni-- packingv inthe.

formity tube.

For this reason a definite of distribution of they preferred limit in cross sectional area cannot be' given. However,

for instance by testit is easy of determination, ing the emciency of a single tube by any approved method. for instance as setforth in In` dustrial and Engineering Chemistry, November 1934, page' 1169.

It may be stated as a general rule that one should proceed with caution after exceeding a cross sectional area of about three square inches although, as shown Iin the article ljust ,referred to, larger cross sectional areas may in some cases be employed without an inordinate loss of eiilciency.

Tubes II are illustrated as by a shell Il which is secured to flanges I4 and I5. Shell. i 1, may be lagged to make the contacting section of the tower adiabatic. However, the lagging may be applied directly to each tube or may include all of the tubes if desired. Any other means may be substituted.

Section BB is a phase contacting section and functions as such.

Below section BB is section AA.

Among the functions of section AA is that of metering vapors into the tubes II, 'Ihese vapors flowing from a still or other source enter the tower through a chamber I8 which is shown being surrounded attached to the lower end of section AA as il` lustrated at I9.

The lower portion of section AA is illustrated as comprising a shell 20 in which is disposed a vapor mixing plate 2l having an opening 22 at its center.

Transverse plate 23 contacts the top of shell is member 24 which in turn contacts header I3.

Member 24 has a plurality of vertically arranged chambers 25 of the samenumber as the tubes I I.- Each chamber 25 communicates with a tube II at its lower end.

anges I4 and I5 respec- Within each chamber 25 is a hollow plug 28 which is shown threaded at 21 into plate 23. The lower end of plug 26 holds the upper end of a metering tube 28 which projects down into shell 29.

A reflux drain tube 29, shown with its upper end secured inplate 23, extends downwardly from each chamber 25 and through plate 2| .into chamber I8. Each tube 29 is provided with a cup 39 about its lower end for purposes which will hereinafter appear.

Section CC is disposed above section BB.

Section CC comprises a plurality of individual condensers. These condensers correspond in number to the tubes I|. As illustrated, each condenser comprises a tubular member 35 which .communicates at its lower end with a separate tube of Vsection BB.

Tubular members 35 are illustrated as being mounted in headers 31 and 38. Headers 31 and 38 are illustrated for convenience as being integral with flanges 39 and 49 respectively. A shell 4| surrounds tubes 35 and contacts anges 39 and 49 to form a chamber 42 for heat exchange purposes.

Shell 4| is illustrated as-having openings 43 for the circulation of a cooling uid through the chamber 42. For effective distribution of the cooling fluid, baiiles 46 each forming an opening 41 with shell 4I, are shown arranged in'spaced relationship in chamber 42 with the openings 41 staggered so as to cause the cooling uid to flow back and forth through the chamber 82 as it Apasses therethrough.

The upper ends of tubes 35 open into chamber 48 which has an opening 49 for the removal of rectified vapors.-

Condenser 5| is connected to vapor outlet 49 by a vapor line 52 and product' receiver 53 is connected to condenser v5| by product line 54.

A bypass 55 is connected to line 54 in which is connected still 56 of a small distilling unit 51 Athe arrangement being such that a small sample of the product flows through still 56 preferably continuously and then back to line 54 or receiver 53.

Distilling unit 51 besides still 55 comprises a small fractionating tower 58 and a condenser 59. Tower 58 may have any desired number of theoretically perfect plates, lsay for instance from six to ten.

A thermocouple 59 is shown threaded through column 58 with junctions 6| and 62 positioned at the top and bottom of the column respectively and ending outside of column 58 at terminals 63 and 64. The remainder of the circuit as shown comprises wire 68, rheostat 61, coil 68 of galvanometer 69 and wire 19. i

Galvanometer 69 is of a well-known type and is illustrated diagrammatically. An essential feature'of galvanometer 69 is that coil 68 rotates in response to and through an arc proportional to Y quantum of current flow and returns to its original position upon the cessation of such flow. Coil 68 carries a mirror 1| which is adapted to reflect a beam of light from a light source 12 in the general direction of photoelectric cell 13 said beam being directed on and olf of said cell depending upon the position of coil 98.

Since it is desired to concentrate the beam on the photoelectric cell for all values of current above a certain point a stop 15 is provided for coil 68 said stop limiting the rotation of coil 68 in a manner to obtain these results.

Cell 13 is a part of a vacuum tube relay circuit.

This circuit comprises a three-element tube 'l1 having a plate 18, a grid 19, and a filament 80. The filament is illustrated as being supplied with alternating current from a transformer 8| for the purposes of heating. The conventional potentiometer 82 with sliding tap 83 is shown connected across the lament terminals, the tap being connected to the minus-B terminal.

The input circuit includes a potentiometer 94 connected across a suitable voltage source with the plus terminal connected to the filament through tap 83 and potentiometer 82. Potentiometer 84 has two sliding taps 85 and 86, taps 85 being connected to grid 19 through cell 13, and tap 86 being connected to grid 19 through the grid leak 81. Tap 85 is directly connected to the cathode 88 of cell 13, and grid 19 is directly connected to anode 89 of cell 13. The particular photoelectric cell illustrated is of the photoemissive type.

A relay 9| is connected in the output circuit and is operated thereby. As illustrated armature 92 breaks a circuit through contacts 93 and 94 when the relay is energized and makes a circuit through these contacts when the relay is deenergized.

The circuit of contacts 93 and 94 comprises wire 95, battery 96, wire 91, solenoid 99, Wire 98, and armature 92.

Solenoid 99 operates valve |90 in bypass |ll| around valve |92 in line |93' which supplies cooling fluid to chamber 42 for the operation of condensers 35.

Assuming` that the individual fractionating units and condensers 35 are at least substantially equally matched as to capacity and efciency, the operation of the invention is as follows: v

Vapors enter chamber |8 from a still or other source and are thoroughly mixed as they pass through opening 22- in plate 2|.

These vapors are metered into plugs 26 by metering tubes 28 which, under the assumed conditions, may be of equal capacity although adjustments may be made, for instance; by making metering tubes 28 interchangeable to compensate for inequalities in the fractionating units as will appear hereinafter.

Plugs 26 are provided with openings 3| in their side faces to permit the vapors to escape into chambers 25 and to prevent descending liquid Ifrom entering the metering tubes 29. From each chamber 25 the vapors pass up through the corresponding tube wherein the desired rectificationtakes place.

When tubes I are' packed and especially when the packing is continuous, the phases will contact each other essentially in i'llm form. Depending upon the rate of reux flow, the reflux, which is conducted down through each tube over the packing medium, will be maintained either en;- tirely in film form or with a portion alternately in film and drop form. The latter also affords efficient fractionation because of a sort of kneading action caused by the drops recontacting the' packing and respreading out into lms only to be followed by the formation of more drops. This brings a large proportion of the liquid particles to the surface for contact with ascending vapors.

Rectied vapors escaping from the upper en ds of tubes enter the corresponding condensers 35 wherein fractional condensation is effected, the condensate in each condenser 35 owing back into the corresponding tube as reiiux condensate and the uncondensed vapors escaping ,the latter case, in View of into chamber 48 wherein all of said vapors commingle. v

'I'he liquid that flows out of each tube Il at its bottom collects in the corresponding chamber and drains down into chamber I8 through the corresponding tube 28.

The purpose of cups 38 is to to prevent tubes 29 and will stand at a certain height therein depending upon the pressure drop. Cups 30 are preferably of sucient capacity to furnish the required amount of liquid for tubes 28 at the time of starting, thus making it unnecessary to depend upon descending reflux for this purpose. Thus the tower will reach equilibrium conditions in a shorter length of time.

If desired any dilferences in the individualfractionating units ||A may be compensated for by adjusting the vapor flow to each unit by interchanging metering tubes 28. This might also be done to a certain extent without an interchange of tubes 28 by making the pressure drop through tubes 28 relatively large, for instance, at least ve times the average resistance to. vapor ow through theindividual fractionating units'. In the relatively larger metering tubes 28 individual units H pressure drop through the any small differences between are minimized. A

Vapors collecting in chamber 48 escape through 49 and are condensed in condenser 5i. The condensate ows through line 54 directly to receiver 53 except thatv portion which flows by means of by-pass 55 through still 58. The product in still 548 is thus continuously replaced.

The liquid in still 56 is kept at a boil by any.

ture diierential between the top and bottom of tower 58 is a measure of the diierence in composition or, in other words, is la measure of the temperature spread of the product.

This temperature diierential may be availed of to control the degree of fractional condensation eiected-in condensers so as to increase the volume of vapors condensed with increase in temperature differential and to decrease the volume of vapors condensed with decrease in temperature dilerential. Thus the product may be made to have .the desired temperature spread.

This temperature spread may be of any desired value starting with zero which is the temperature spread of a constant boiling substance.

The operation of the circuit for controlling the condensing effect of condensers 35 in accordancel with the temperature differential between junctions 6| and 62 is as follows:

A diierence in temperature between points 8| and 82 generates an electromotive force which in turn causes current ow through coil 680i galvanometer 69. As a result coil 88 will rotate through an arc proportional to the quantum of current iow. Whether or not the reflected beam of light will be focused on cathode 88 `of photoy ceu 13.

will depend upon the'value o1' differential and the adjustment The circuit is adjusted by means which controls the amount of current for any given temperatureV diiferential. The adjustment is such that the beam of light Willbe focused on cathode 88 when and as long as the desired temperature Vspread is exceeded.

electric cell 73 the temperature of the circuit. of rheostat 81 beam of light, suicient current will ow through the output .circuit to operate relay 9| to hold contacts 93 and 94 apart. This permits valve |88 toy assume a closedposition to prevent cooling fluid from passing through bypass |8|. The size of this current iti-the output circuit may be adjusted at tap 88 which controls the normal grid bias.

The setting of valve |02 is such that when valve |08 is closed the cooling fluid supplied to chamber 42 is slightly below requirements.

Now, let us assume that a temperature spread cathode 88 when the spread is at 10. Now, should the spread increase beyond 10 the resulting increase in temperature differential will increase the electromotive force generated by the thermolight onto cathode 88, thereby making the cell 'I3 conductive. This will increase the grid bias open valve |88 to permit additional cooling fluid to flow tochamber 82.

vAri increase in the flow of cooling fluid to chamber 82 increases the volume of vapors condensed by condensers 35 and consequently the volume of reiiux condensate both of which act to decrease the temperature spread.

As soon as the temperature spread has decreased suficiently the light beam will move to one side of cathode 88 to open the circuit through 9| thereby breaking the circuit through solenoid 99 and closing valve |00. This cycle repeats itself continually. i

After the device is in operation rheostat 61 may be manipulated as required for'ner adjustment.

In view` of the high sensitivity of thermocouple and galvanometer circuits, only a very small in temperature differential is required and close valve |08.

on or off of cathode`88.

Since a sample of the product preferably ows continuously and in small amount through the still 56 the overall composition of the components in column 58 will follow closely the overall composition of the product.

Condenser 59- is operated as a-partial condenser or as a total condenser to `prevent losses.

Tower I0 may be operated at any desired pressure whether atmospheric, suliatmospheric or superatmospheric, and column 58 is preferably operated at the same pressure as column I0.

Any other type of valve or other device might be substituted. for valve |00, for instance, a valve adapted to increase and decrease its opening, or a device adapted to increase` and decrease the pressure causing the ow of cooling fluid, according to requirements. Furthermore, any other circuit might be substituted for that described. To effect especially rapid heat exchange and to increase the degree of rectification, tubes 35 if vdesired may be packed, for instance as illustrated at |05, with any suitable packing materials such as raschig rings, ,jack chain, etc. or with special types of packing. elements, for instance the packing elements described and claimed in Patent 2,037,317, granted April 14, 1936.

In order to further increase the rate of heat exchange by the elimination of surface films these packing elements may be joined together and/or to the tube walls.

To increase the rate of heat exchange still further, chamber 42 might also be packed, for instance as illustrated at |06, with any suitable packing materials, and this packing might also be joined into an integral mass-and/or to the outer walls of tube 35 to eliminate surface As illustrated, baffles 40 cause the heating fluid to flow through acircuitous course through chamber 42. Any other suitable arrangement may be substituted.

It is simpler to make tubes of `the same cross section and length, to provide the 'same type of contacting means in each tube, to feed vapors t'o be fractioned at substantially the same rate to each tube, and to cause reiiux condensate to form at substantially the same rate in each condenser 35. v

However, the individual fractionating units and/or the individual condensers 35 may differ without departing fromthe spirit of the invention. Such differences may be in construction such as in size, length, contacting means, Ior

4vary as to construction otherwise.

For instance, the individual fractionating units Il and/or their associated condensers 35 may but may be matched so that each condenser 35 will deliver rectied vapors of substantially the same composition when vapors'are fed at substantially the same rate to each fractionating unit and reux condensate is formed at substantially the same rate in each condenser 35.

On the other hand the individual fractionating units and/or the individual condensers 35 may be of the same and/or of different construction but may differ as to capacity. In this case adjustments of the vapor feed to fractionating units and/o1.` of the condensing capacity of condensers 35 may be made to cause the rectified vapors leaving any condenser 35 to be of at leastsubstantially the same composition as the rectified vapors leaving any other condenser 35.

The use of metering tubes 28 makes it possible to adjust the feeding rate of vapors to any fractionating unitA by employing a metering tube for that unit of the desired capacity. Likewise, the condenser 35 for any fractionating unit may be especially constructed to have the desired condensing capacity. i

Thus the desired balance may be obtained. The precision of this balance will, of course, depend upon the results desired and, therefore, may be rough or close according to requirements.

Other variations are possible. For instance, if fractionating units are of the same cross section and together with their `associated condensers are equally matched as to pressure drop, section A may be omitted entirely. The ascending vapors, due to the uniformity of pressure drop, will divide equally between the various tubes However, should there be differences in pressure drop when section A or a device of equivalent function is omitted, thismight be compensated for by adjusting the condensing capacity of individual condensers 35 to adjust the quantityv of reflux condensate descending into the individual tubes Il to obtain rectified vapors of at least substantially the same composition from each condenser 35.

Ifthe tubes are of different cross sectional area when section A is omitted the pressure drops through the individual tubes or the reflux condensate descending into the individual tubes or both might be adjusted to obtain rectified vapors from each condenser 35 of the desired composition. l

Other possible variations will suggest themselves to persons skilled in the art upon becoming familiar With this invention.

As previously described, adjustments of rheostat 01 are made to obtain a product of the desired temperature spread. In order to facilitate the adjustment of rheostat 61 a second thermocouple |08 might be inserted in column 50 with junctions |09 and ||0 positioned similarly to junctions 6| and 02. Thermocouple |08 might operate a meter calibrated to read directly in degrees of temperature spread.

While in the particular description the product is withdrawn as vapor, it is to be understood that any.other means known in the art may be employed for the separation of product.

Although4 the feed into the tower has been shown at the bottom thereof, the feed may be at any other point or points and may be in the vapor or liquid phase according to the type and point of feed. The feed material would be, of course, preferably metered into the fractionating units following the principles of feed discussed above.

Valve |00 or any other device broadly producing a similar result might be employed for controlling any other means for varying the condensing effect of condensers 35. For instance,

valve |00 might b e employed in a line for leading a relatively colder solution into line |03 so as to make the device more sensitive.

Instead of the fluid entering chamber 42 being such that it absorbsonly sensible heat, that is, it only rises in temperature as it flows through condenser section CC, this fluid may be so chosen that it undergoes evaporation or boiling about tubes 35 so that the cooling of tubes 35 is prncipally due vto vaporization of the fluid. These vapors then pass out at upper opening 43 of shell 4| to a vapor liquefier such as condenser and/compressor (not shown) and are liquified and let back into line |03 to repeat the cycle.

In this type of operation baies 46 are preferable removed. A liquid of suitable boiling point is introduced into chamber 42 and its boiling point is so chosen that `this liquid is boiled by vapor condensing inside 4of tubes 35. This liquic' while boiling preferably stands at a vreasonable height above tube sheet 38, so that it completelj surrounds all tubes 35, and there is local boiling about each tube 35 thereby effecting condensation of vapors in each tube 35. The vapors "of this boiling liquid pass up around tubes 35 and out of chamber 42 into a vapor liquefier (not shown) where they are liquefied and returned as liquid to |03. The amount of this liquid introduced about tubes 35 is controlled by valve 02 and electrically operated valve |00.

Valve automatically keeps the desired amount of liquid standing above tube sheet 38.

Increasing the height of liquid standing above tube. sheet 38 and surrounding tubes 35 condenses more vapors to liquid inside tubes 35 thereby increasing the reflux ratio in the column as a whole assuming the rate of vapor entry to chamber 8 is constant. This will decrease the temperature spread and in turn the amount of fluid owing through valve |00.

This cycle repeats itself continually and by proper adjustment the desired height of liquid in chamber 42 may be maintained.

Reducing the height of liquid about tubes 35 condenses less in these tubes lowering the reux ratio in the column as a whole on the basis that a constant inow of vapors enters I8. This will increase the temperature spread and in turn the amount of uid owing. through valve |00.

In this way the fractionating .column I0 is made to function to produce the desired product whether the operation be batch or continuous.

Again, a separate liquid might ow through |00 and another liquid flow through |02, both these liquids mixing and owing into chamber ,42 where they are vaporized as before. `A higher boiling liquid may now through |02 and a lower boiling one through |00. The ow of higher boiling liquid is such that it produces the lowest redux that is desired for operation of column I7 while the total possible iiow (if valve |00 were open) of low boilingliq'uid through valve 00 is such that it produces the highest reiiux desired for operation of column Il. Valve .|00 then intermittently operates to give a liquid mixture of suitable boiling point to enable the desired reux to be obtained so producing the desired type of product escaping from 49.

The mixed vapors escaping from chamber 42 are then led to a fractionatng column (not shown) which resolves this mixture into the two liquids which are then separately returned to valves |00 and |02 to repeat the cycle.

Thus, there is ample means of employing the controlv mechanism to condense the desired amount of vapors inside tubes 35.

Condensers 35 and/or chamber 42 or their equivalent might be constructed in any other,

manner. For instance, condensers 35 might be separately encased to form separate cooling chambers into each of which the cooling uid might be metered particularly if it is desired to individually control the condensing capacity of the condensers 35.

Likewise, any other device performing the function of the control mechanism for valve |00 or its equivalent might be substituted.

For instance, any other .means for measuring the temperature spread of the product might be substituted to control the vacuum tube circuit operating valve |00 or any other type ofcontrol for the iiuid entering chamber 42 might be employed.

While a tower has been particularly described herein it is to be understood that the invention in its broad phases covers a tower of any construction to which the inventionV might be adapted.

` adiabatic conditions as realized It is to be understood that tower |0 might be varied in construction, for instance, for delivering one or more side streams.

It should be noted that in the form shown each individual contacting unit is in heat exchange relationship with each other individual contacting unit so that heat equilibrium is possible.

Furthermore, it is possible to feed vapors from a still or other source into the heat exchange chamber to attain uniformity and control of temperature about the contacting units.

Many other variations are possible.

'While a particular form mechanism have been shown and described it is to be understood that the invention is capable of broad application.

The tower might be employed for the contacting of liquid phases, for instance, by introducing a solution of solvent and' oil into .the tower in place of the vapors and by precipitating oil from the solution by cooling the solution in the condenser section. Due to a difference in density the precipitate will ow through the tower countercurrently to the solution much the same` as condensate in the case of distillation. The solution remaining after the precipitation might be run through a colorimeter'having its light adjusted so as to fall upon the photoelectric cell of the circuit disclosed in the drawings. This circuit might then be adjusted so as to increase the cooling eect of the condenser section to cause greater 'reflux with increase in transparency of the solution and to decrease the cooling effect to cause less reflux with decrease in. transparency of the solution thus controlling the composition of the extract in solution.

The solution might be stripped of a part or all of'. the solvent prior to passing through the colorlmeter.

Such an arrangement would be particularly useful in processing lubricating oil derived from Pennsylvania grade crude since the color of the extract in such cases varies rapidly. n The control might also be made to follow the viscosity at any desired temperaturevfor instance at 100 F. of either the raflinate or the extract since both vary rapidly in viscosities with change in percentage of extract. 'Ihis might be accomplished, for instance by stripping either the extract or rainate of solvent and forcing the oil by means of aA constant displacement pump through a capillary at the desired temperature. The control might then be operated by the pressure drop across the capillary to control the cooling effect of the condenser and consequently the composition of the extract.

The rafllnate,. of course, will be that oil portion which is removed from the tower as reflux.

In the foregoing it willbe understood that the tower will be constructedwith the condenser at the top when the solution is lighter than the oil separated by the condenser and will be constructed with the condenser at the bottom when the solution is heavier than the oil separated by the condenser.

Many other modifications might be made.

The term adiabatic conditions as used in the claims is intended to define conditions of an isolated thermodynamic system arranged such that for practicable purposes-no heat enters or leaves it. The term, therefore, includes not only true adiabatic conditions but also substantially in practice.

Having particularly described the invention, it is to be understood that changes, omissions, addiof tower and control tions, substitutions and/or modications might be made therein within the scope of the claims without departing from the spirit thereof.

I claim: v

1. A process for fractionating a mixture comprising, owing said mixture in the vapor phase Y through a plurality of fractionating units countercurrently to a liquid phase while maintaining said fractionating units under adiabatic conditions, separately subjecting the rectied vapors produced by each individual fractionating unit to fractional condensation in an individual condenser to produce said liquid phase for said individual fractionating unit, combining the remaining uncondensed vapors to produce the product, and increasing and decreasing the volume of condensate formed by said individual condensers with increase and decreaseof the temperature spreadl of said product about the desired value.

2. A process for fractionating a mixture comprising, owing said mixture in the vapor phase through a plurality of fractionating units of relatively small cross sectional area countercurrently to a liquid phase While maintaining said fractionating units under adiabatic conditions, separately subiecting the rectified vapors produced by each individual fractionating unit to iractional condensation in an individual condenser to produce said liquid phase for said individual fractionating unit, combining the remaining uncondensed vapors to produce the product, and increasing and decreasing the volume of condensate formed by said individual condensers with increase and decrease of the temperature spread of said product about the desired value.

3. A process for fractionating a mixture comprising, flowing said mixture in the vapor phase through a plurality of iractionating units counter-currently to a liquid phase while maintaining said fractionating units under adiabatic conditions, separately subjecting the rectified vapors produced by each individual fractionating unit to fractional condensation in an individual condenser to produce said liquidl phase for said individual fractionating unit, combining the remaining uncondensed vapors to produce the product, and increasing and decreasing the volume of condensate formed by said individual condensers with increase and decrease of the temperature spread of said product about the desired value by separately fractionating a sample of said product and' measuring change in temperature spread through change in diiferential of composition of materials concentrated at different points in said last mentioned fractionating zone.

4. A process for fractionating'a mixture comprising, flowing said mixture in the vapor phase through a plurality of fractionating units of relatively small cr`oss sectional area countercurrently to a liquid phase While maintaining said fractionating units under adiabatic conditions, separately subjecting the rectified vapors produced by each individual fractionating unit to fractional condensation in an individual condenser to produce said liquid phase for said individual fractionating unit, combining the remaining uncondensed vapors to produce the product, and increasing and decreasing the volume of condensate formed by said individual condensers with increase and decrease of the temperature spread vof said product about thedesired value by separately fractionating a sample of said product and measuring change in temperature spread through change in differential of composition of materials concentrated at different points in said last mentioned fractionating zone. y

v5. Apparatus comprising a plurality of individual fractionating units, an individual partial condenser for each fractionating unit, means common to said condensers for controlling the condensing capacity thereof, means for sampling the combined product produced by said individual fractionating units and partial condensers, and means for controlling said first mentioned means through said second mentioned means.

6. Apparatus comprising a plurality of individual fractionating units of relatively small cross sectional area, an individual partial condenser for each ractionating unit, means common to said condensers for controlling the condensing capacity thereof, means for sampling the combined product produced by said individual fractionating units and partial condensers, and means for controlling said iirst mentioned means through said second mentioned means.

'7. Apparatus comprising a plurality of individual fractionating units ofrelatively small cross sectional area, said fractionating units being of at least substantially equal capacity and efciency, an individual partial condenser for each fractionating unit, said partial condensers being of at least substantially equal capacity and eiciency, means for supplying cooling fluid'at least substantially equally to said partial condensers, means for combining the vapors escaping from said partial condensers to produce the product, means for separately fractionating a sample of saidproduct,

and means responsive to increase and decrease inl differential of composition of materials concentrated in different sections of the fractionating zone of said last mentioned means for respectively increasing and decreasing the cooling rate of said cooling fluid.

8. A process for fractionating a mixture cornprising, owing said mixture in the lvapor phase through a plurality of fractionating units countercurrently to a liquid phase While maintaining said fractionating units under adiabatic conditions, separately subjecting the rectified vapors produced by each individual fractionating unit to fractional condensation in 'an individual condenser to produce saidliquid phase for said individual fractionatng unit, combining the remaining uncondensed vapors to produce the product, increasing and decreasing the volume of condensate formed by said individual condensers with increase and decrease of the temperature spread of said product about the desired value, and maintaining the individual fractionating units in heat exchange relationship with each other so as to at least approach heat equilibrium between said units.

9. Apparatus comprising a plurality of individual fractionating units, an individual partial condenser for each fractionating unit, means common to said condensers for controlling the condensing capacity thereof, means for sampling the combined product produced by said individual fractionating units and partial condensers, means for controlling said iirst mentioned means through said second mentioned means, and means for holding said individual fractionating units in heat exchange relatio ship-with each other.

MERRELL R. FENSKE. 

